JP5925105B2 - Saturator and natural gas reforming system having the same - Google Patents

Description

  The present invention relates to a saturator that adds water vapor to a gas. The present invention also relates to a natural gas reforming system including the saturator.

  In the process of synthesizing liquid hydrocarbons such as methanol and kerosene and light oil (Fischer-Tropsch process), as described in Patent Document 1 and Patent Document 2, steam is added to hydrocarbon gas such as natural gas. And reformed to produce synthesis gas containing hydrogen, carbon monoxide and carbon dioxide. As a method of adding water vapor to the gas in the above process, there is a method of humidifying natural gas using a saturator in addition to a method of adding steam directly to natural gas.

  Further, in a gas turbine that adds steam to the combustion gas, a saturator may be installed to humidify the combustion gas.

  The saturator recovers heat from another heat source (gas) in the heat exchanger, heats the gas flowing through the saturator using the recovered heat, and sprays water into the gas to evaporate it. Steam is added to.

JP 2003-34660 A JP 2004-277186 A

  The saturator is required to recover heat more efficiently from another heat source. For example, when a saturator is installed in a process for reforming natural gas, the saturator is heated at a high temperature including water vapor at a saturated vapor pressure in which low-temperature natural gas sprayed with water is heated by heat exchange with high-temperature synthesis gas. A configuration that is discharged as natural gas is adopted. However, it was considered that there was room to effectively recover heat from the synthesis gas to a lower temperature range.

  Further, in order to reliably reform the raw material gas with water vapor, it is necessary to add surplus water vapor with respect to the amount of carbon. When the temperature of the saturated raw material gas after passing through the saturator is low, the amount of water vapor contained is insufficient with respect to the required amount, so it is necessary to add water vapor separately before transporting to the reformer. Therefore, the saturator is required to discharge saturated gas having more water vapor humidified at a high temperature.

  An object of the present invention is to provide a saturator that can recover and utilize heat recovery from a heat source more efficiently and can add water vapor to a gas (fluid) to the maximum extent.

  One aspect of the present invention includes a flow passage through which a first fluid circulates, and one or a plurality of flow passages disposed along the flow direction of the first fluid in the flow passage, wherein the first fluid and the second fluid A first heat exchange section that exchanges heat between the first heat exchange section and the first fluid exchange section in the flow direction in the flow passage, and after passing through the first heat exchange section A second heat exchange section for exchanging heat between the first fluid and the third fluid; and the upstream side of the first fluid in the first heat exchange section and the second heat exchange section, in the flow passage. A humidifying unit that adds water to the first fluid that circulates, and the third fluid that has been subjected to heat exchange in the second heat exchange unit are transferred from the second heat exchange unit to the first heat exchange unit. A transport path that transports one fluid upstream and flows into the flow path as the first fluid, in the first heat exchange section, The first fluid is heated and humidified, the second fluid is cooled and discharged out of the system, and in the second heat exchange section, the first fluid is heated and humidified to a saturated vapor pressure. The saturator is discharged out of the system and the third fluid is cooled.

  The said aspect WHEREIN: It is preferable that the said flow path is one tower which accommodates the said 1st heat exchange part and the said 2nd heat exchange part.

  Or in the said aspect, the said flow path is piping which connects these containers and these containers, and the said 1st heat exchange part and the said 2nd heat exchange part are accommodated in the said container one each. Is preferred.

In the saturator of the above aspect, a plurality of heat exchange units are installed in the flow passage. In the second heat exchange unit, the high-temperature third fluid that is the same gas as the first fluid is used for heating and humidifying the first fluid immediately before being discharged from the saturator. Further, the third fluid flows into the saturator flow passage as the first fluid, and is used for cooling the second fluid in the first heat exchange section.
By setting it as said structure, while the temperature of the 1st fluid discharged | emitted from a saturator can be made high, the temperature of a 2nd fluid can be made low. Therefore, the efficiency of heat recovery in the system is improved. Moreover, lowering the temperature of the second fluid is preferable because it leads to a reduction in the amount of waste heat from the second fluid in the downstream of the saturator.

  Another aspect of the present invention is a reformer that reacts natural gas, which is the first fluid, with water vapor to generate a synthesis gas containing hydrogen, carbon monoxide, and carbon dioxide, which is the second fluid. A natural gas reforming system comprising a tank for storing natural gas to be the third fluid, and the saturator of the above aspect.

  For example, when the saturator is installed in a natural gas reforming system, it becomes possible to reduce the amount of water vapor added from outside the system (for example, a boiler) to the humidified natural gas (first fluid). Driving efficiency can be improved.

  According to the present invention, the temperature of the first fluid discharged from the saturator is further increased, and the temperature of the second fluid is further decreased. That is, the saturator of the present invention can perform heat recovery superior to the conventional product, and can improve the thermal efficiency of the entire system.

  If the saturator of the present invention is installed in a natural gas reforming system, the amount of water vapor added from outside the system to natural gas, which is a raw material gas, can be reduced, and the consumption of natural gas, which is a production raw material, is reduced. be able to.

1 is a schematic view of a natural gas reforming system. 2 is a schematic diagram of a saturator of case 1. FIG. 3 is a schematic view of a saturator of case 2. FIG. 3 is a schematic view of a saturator of case 3. FIG. It is the schematic of an example of the saturator of 2nd Embodiment.

  The saturator of the present invention is applied to a methanol synthesis system or a liquid hydrocarbon synthesis system that adds water vapor to a raw material gas, or a gas turbine that adds water vapor to combustion gas or combustion air.

Hereinafter, embodiments of the saturator of the present invention will be described by taking a natural gas reforming (steam reforming) system as an example.
FIG. 1 is a schematic diagram of a natural gas reforming system. The natural gas reforming system 1 includes a reformer 2, a waste heat boiler 9, a natural gas supply line 10, and a saturator 20.

  The reformer 2 includes a reaction tube 3, a reforming furnace 4, a waste heat recovery unit 5, and a chimney 6. The reaction tube 3 is installed in the reforming furnace 4. The reaction tube 3 is filled with a catalyst (for example, a nickel catalyst). The reaction tube 3 is connected to the saturator 20 by a pipe 7. The pipe 7 is configured to pass through the waste heat recovery unit 5. The reaction tube 3 is connected to the saturator 20 via the waste heat boiler 9 by the pipe 8.

  Fuel gas (for example, natural gas) and air are supplied to the reforming furnace 4 from a pipe (not shown). The reaction tube 3 is heated to about 850 to 900 ° C. by the combustion of the fuel gas in the reforming furnace 4. The combustion exhaust gas in the reforming furnace 4 is conveyed to the chimney 6 through the waste heat recovery unit 5 and is discharged from the chimney 6 to the outside of the reformer 2.

  The natural gas supply line 10 is connected to the saturator 20. The natural gas supply line 10 is connected to a natural gas supply source (not shown).

[First Embodiment]
<Case 1>
FIG. 2 is a schematic view of an example (case 1) of the saturator of the first embodiment. In the saturator 20 of the case 1, first heat exchange units 22 a and 22 b and a second heat exchange unit 23 are installed in a tower 21. The first fluid flows through the tower 21 from the upper side to the lower side. That is, the tower 21 is a flow passage through which the first fluid flows. In the case of a saturator installed in the natural gas reforming system 1, the first fluid is natural gas.

  The first heat exchange units 22a and 22b are shell-type heat exchangers. In the shell-type heat exchanger, a plurality of tubes are arranged on the outer periphery of the tower 21 and the second fluid flows through the tubes. In the case of a saturator installed in the natural gas reforming system 1, the second fluid is a synthesis gas fed from the reaction tube 3. In the first heat exchange units 22a and 22b, the first fluid and the second fluid exchange heat without contact.

  One or more first heat exchange units are installed along the flow direction of the first fluid. The saturator 20 of the case 1 has a configuration in which two first heat exchange units are provided. When installing a some 1st heat exchange part, the adjacent 1st heat exchange part 22a, 22b is connected by the piping 24. FIG. The second fluid flows through the pipe 24. In the saturator 20 of FIG. 2, the second fluid flows into the saturator 20 from the first heat exchange part 22b on the downstream side of the first fluid, and is discharged out of the saturator 20 from the first heat exchange part 22a on the upstream side of the first fluid. Is done.

  The 2nd heat exchange part 23 is installed in the 1st fluid downstream of 1st heat exchange part 22a, 22b. The second heat exchange unit 23 is a shell-type heat exchanger, and the third fluid circulates in the tube on the outer periphery of the tower 21. In the case of a saturator installed in the natural gas reforming system 1, the third fluid is natural gas (raw gas). The third fluid is supplied from the natural gas supply line 10. In the second heat exchange unit 23, the first fluid and the third fluid exchange heat without contact.

  The second heat exchange unit 23 is connected to the upper portion of the tower 21 through the conveyance path 25. The third fluid flows through the conveyance path 25. The third fluid flows into the tower 21 from the top of the tower 21 and circulates in the tower 21 as the first fluid.

  The humidifying units 26a, 26b, and 26c are installed in the first heat exchange units 22a and 22b and the second heat exchange unit 23, respectively. The humidifying units 26a, 26b, and 26c are spraying units (not shown) that spray water on the first fluid that circulates in the tower 21, and storage units 27a, 27b that collect and store the sprayed surplus water and condensed water. 27c and pumps 28a, 28b, 28c that circulate the water in the storage units 27a, 27b, 27c to the spraying unit. The spreading unit is installed on the first fluid upstream side of the first heat exchange units 22 a and 22 b and the second heat exchange unit 23.

  A pipe 29 is connected on the upstream side of the first heat exchange units 22 a and 22 b and the second heat exchange unit 23. Water is supplied from the outside of the saturator 20 to the first fluid from the pipe 29. The water supplied from the pipe 29 may be industrial water, or may be condensed water generated when the second fluid discharged from the first heat exchanger 22a to the outside of the saturator 20 is further cooled.

Below, the example which humidifies natural gas is shown and the process of humidifying gas using the saturator 20 of case 1 is demonstrated.
As the third fluid, high-temperature natural gas flows into the second heat exchange unit 23. The third fluid is heated, for example, by passing from the natural gas supply line 10 through the waste heat recovery unit 5 of the reformer 2. Specifically, the temperature of the third fluid before flowing into the second heat exchange unit 23 is raised to about 380 ° C. to 400 ° C. (temperature T ₁ ). Note that the third fluid contains almost no water vapor.

In the second heat exchange section 23, heat exchange is performed between the first fluid (temperature T ₉ ) flowing through the tower 21 and the third fluid. The heat exchanger, the third fluid is cooled to a temperature T _2.

Third fluid that has been cooled to a temperature T ₂ flows through the conveying path 25, and flows as the first fluid to the tower 21 top of collar tower 21. The first fluid flows in the tower 21 from the upper part of the tower 21 downward.

The spraying part of the humidifying part 26a sprays water on the first fluid before flowing into the first heat exchanging part 22a. The sprayed water comes into contact with the first fluid (temperature T ₂ ) and evaporates, and water vapor is added to the first fluid. At the same time, the first fluid is cooled to a temperature T ₃ by heat of vaporization. At this time, if the first fluid contains water vapor with a saturated vapor pressure, this leads to an increase in heat recovery efficiency and a decrease in the amount of water added from outside the system, which will be described later, and the energy efficiency of the natural gas reforming system 1 as a whole. Is advantageous.

Syngas is generated in the reaction tube 3 of the reformer 2 as the second fluid.
Natural gas (including hydrocarbons mainly composed of CH ₄ ) humidified by the saturator 20 through the following steps is supplied from the pipe 7 to the reaction pipe 3. In the reaction tube, the hydrocarbon in the natural gas reacts with water vapor to generate carbon monoxide (CO) and hydrogen (H ₂ ). The generated CO further reacts with water vapor to generate carbon dioxide (CO ₂ ) and H ₂ . That is, the synthesis gas comprises _H 2, CO, CO _2, and water vapor.

The synthesis gas discharged from the reaction tube 3 is cooled by the waste heat boiler 9 through the pipe 8 and then conveyed to the saturator 20. Specifically, the synthesis gas discharged from the reformer 2 at 850 to 900 ° C. is cooled to about 300 to 400 ° C. (temperature T ₁₁ ) by passing through the waste heat boiler 9, and then the second gas of the saturator 20. 1 is supplied to the heat exchange unit 22b.

  As the second fluid, the synthesis gas flows into the first heat exchange unit 22b. The 2nd fluid which distribute | circulated the 1st heat exchange part 22b flows in into the 1st heat exchange part 22a via the piping 24. FIG. The second fluid that has circulated through the first heat exchange unit 22a is discharged to the outside of the saturator 20.

In the first heat exchange units 22a and 22b, heat exchange is performed between the first fluid and the second fluid flowing in the tower 21. The first fluid is heated by the heat exchange. On the other hand, the second fluid is cooled. In case 1, the first fluid is heated from an inlet temperature _{T 3} on the outlet temperature _{T 4} at the first heat exchanging portion 22a, is heated from an inlet temperature _{T 5} at the first heat exchanging portion 22b in the outlet temperature _{T 6.} The second fluid is cooled from the temperature _{T 11} to _{T 13} in the first heat exchange portion 22b, it is cooled from the temperature _{T 13} to the temperature _{T 14} in the first heat exchange portion 22a.

In the saturator 20 of case 1, the spraying part of the humidification parts 26a, 26b sprays water into the tower 21 from the upper side of the first heat exchange parts 22a, 22b. The sprayed water becomes water vapor by the heat of the first fluid and the second fluid when passing through the first heat exchange units 22a and 22b. By this step, the first fluid is heated while maintaining the saturated vapor pressure when passing through the first heat exchange units 22a and 22b.
The surplus water and the condensed water sprayed are collected by the storage units 27a and 27b and circulated to the spraying units of the humidifying units 26a and 26b by the pumps 28a and 28b.

First fluid has reached the temperature T ₆ passes through the first heat exchanging portion 22b flows as the temperature T ₉ in the second heat exchange unit 23. In the second heat exchanger 23, the first fluid is heated to a temperature T ₁₀ from the temperature T ₉ Replace third fluid and heat.

  From the upper side of the second heat exchange unit 23, the spraying unit of the humidifying unit 26 c sprays water into the tower 21. The sprayed water becomes water vapor by the heat of the first fluid and the third fluid when passing through the second heat exchange unit 23. By this step, the first fluid is heated while maintaining the saturated vapor pressure when passing through the second heat exchange section 23.

  The first fluid that has passed through the second heat exchanging unit 23 is discharged from the saturator 20 with water vapor having a saturated water vapor pressure, and is transferred to the reaction tube 3 of the reformer 2 through the pipe 7. In the reaction tube 3 described above, the reforming of the natural gas is performed with the amount of water vapor with respect to the amount of carbon in the natural gas being about 2-3. Water vapor may be added to the first fluid in the middle of the pipe 7 so as to achieve the above water vapor ratio.

<Case 2>
FIG. 3 is a schematic view of another example (case 2) of the saturator of the first embodiment. The saturator 30 of the case 2 has the same configuration as the saturator 20 of FIG. 2 except that three first heat exchange units (22a to 22c) are installed and a humidifying unit 26d is installed in the first heat exchange unit 22c. The first heat exchange units 22 a to 22 c are connected by a pipe 24.

In Case 2, in the first heat exchange portion 22c, the first fluid is heated from an inlet temperature _{T 7} to the outlet temperature _{T 8.} The first fluid temperature _{T 8} reaches the second heat exchange section 23 as the temperature _{T 9.} Since the humidifying part 26d sprays water from the upper part of the first heat exchanging part 22c, the first fluid passes through the first heat exchanging part 22c while being heated while maintaining the saturated vapor pressure.

The second fluid flows from the reaction tube 3 of the reformer 2 through the waste heat boiler 9 into the first heat exchange unit 22c. The second fluid is cooled from the temperature _{T 11} to the temperature _{T 12} in the first heat exchange portion 22c is cooled from the temperature _{T 12} to the temperature _{T 13} in the first heat exchange portion 22b, _{T 13} in the first heat exchange portion 22a It is cooled to a temperature _{T 14} from. The second fluid at temperature T ₁₄ is discharged from the saturator 20.

In cases 1 and 2, since the second heat exchange unit is installed and the first fluid is heated using the heat of the third gas which is the same gas and is high temperature, the thermal efficiency of the entire system is improved. The temperature difference ΔT between the temperature T ₉ of the first fluid and the temperature T ₂ of the third fluid can be arbitrarily set under the condition of T ₂ > T ₉ . When the temperature difference ΔT is smaller, the heat of the third fluid can be used for heating the first fluid, which is the same as the third fluid, so that the heat recovery efficiency of the entire system is increased.

The temperature difference ΔT is small, leads to a temperature of T ₂ is low. The lower the temperature T ₂ of the third fluid, it is possible to reduce the temperature T ₃ of the first fluid after the water is sprayed in the first heat exchanging portion 22a upper part of the column 21. The lower the temperature T ₃ of the first fluid, the heat recovery from the second fluid is increased.

Increasing the number of installed first heat exchange unit, can recover more heat from the second fluid, and a lower second fluid temperature T ₁₄ of that discharged from the saturator 20 and 30, the temperature T of the first fluid ₁₀ can be made higher. However, in order to perform heat recovery, the temperature of the second fluid needs to be higher than the temperature of the first fluid in each first heat exchange section. The number of first heat exchange units installed is set as appropriate within a range in which the temperature relationship is established.

<Case 3>
FIG. 4 is a schematic view of a saturator (case 3) as a comparative example. In the saturator 40 of the case 3, one first heat exchange unit 42 is installed in the tower 41, but no second heat exchange unit is installed.

In case 3, the third fluid (temperature T ₁ : 380 to 400 ° C.) flows into the tower 41 as the first fluid from the top of the tower 41. As in the case 1, water from outside the system is supplied to the spraying unit 50 of the humidifying unit 46 through the pipe 49, and water is sprayed from the spraying unit to the first fluid above the first heat exchange unit 42. The spraying of water, the first fluid is cooled to a temperature T _3, the first fluid is humidified to saturation vapor pressure. In the case 3, the surplus water and the condensed water sprayed are collected by the storage unit 47 and circulated to the spraying unit of the humidification unit 46 by the pump 48.

While the first fluid flows through the first heat exchange unit 42, heat exchange is performed between the first fluid and the second fluid. By this step, the first fluid is heated from the temperature T ₃ to the temperature T ₁₀ while maintaining the saturated vapor pressure, and is discharged from the saturator 40. The second fluid is cooled from the temperature T ₁₁ to the temperature T ₁₄ by the heat exchange and is discharged from the saturator 40.

Table 1 shows an example of temperatures T _{1 to} T ₁₄ in the saturators of cases 1 to 3. Cases 1, 2 and 3 have the same conditions for the temperature T ₁ of the third fluid flowing into the saturator and the temperature T ₁₁ of the second fluid.

Cases 1 and 2 are provided with the second heat exchanger 23 to heat the first fluid using the heat of the high-temperature third fluid. 1 the temperature _{T 10} of the fluid is high.
In the case of the natural gas reforming system 1, the first fluid is reformed after further adding steam to the first fluid discharged from the saturator in order to obtain the amount of steam necessary for the generation of synthesis gas as described above. It is fed to the reaction tube 3 of the vessel 2. In cases 1 to 3, the amount of water vapor in the first fluid has a saturated vapor pressure, so that cases 1 and 2 have a larger amount of water vapor in the first fluid discharged from the saturator than case 3. For this reason, when the saturators 20 and 30 of the cases 1 and 2 are installed, the amount of water vapor added from outside the system can be reduced.

Also, since more temperatures in cases 1 and 2 is allowed to flow into a lower third fluid into the tower 21 top, it is possible to reduce the temperature T ₃ of the first fluid in the first heat exchange portion 22a upstream from the case 3 . In cases 1 and 2, the amount of heat recovered from the second fluid is increased by heat exchange in the first heat exchange sections 22a to 22c, the heat efficiency in the system is improved, and the second fluid discharged from the saturator The temperature can be greatly reduced. In the natural gas reforming system 1, the second fluid (syngas) discharged from the saturators 20 and 30 is further cooled, but according to cases 1 and 2, the amount of waste heat from the second fluid on the downstream side Can be reduced.

[Second Embodiment]
FIG. 5 is a schematic diagram of an example of a saturator according to the second embodiment. In FIG. 5, the same components as those in the first embodiment are denoted by the same reference numerals.

  The saturator 60 of the second embodiment includes a plurality of containers 61a to 61c. Shell-type first heat exchange units 22a and 22b are accommodated in the containers 61a and 61b, respectively. The shell-type second heat exchange unit 23 is accommodated in the container 61c.

  The container 61a and the container 61b are connected by a pipe 62a. The container 61b and the container 61c are connected by a pipe 62b. Accordingly, in the second embodiment, the container 61a, the pipe 62a, the container 61b, the pipe 62b, and the container 61c serve as a flow path through which the first fluid flows.

  The second heat exchange unit 23 of the container 61c is connected to the upper part of the container 61a through the transport path 25. The third fluid flows through the conveyance path 25. The third fluid flows into the container 61a from the upper part of the container 61a and flows through the flow passage as the first fluid.

  The container 61a and the container 61b are connected by a pipe 24. The second fluid flows through the tube installed on the outer periphery of the container 61b that accommodates the first heat exchange part 22b, and is installed on the outer periphery of the container 61a that accommodates the first heat exchange part 22a through the pipe 24. After circulating through the tube, it is discharged out of the saturator 60.

  Humidification parts 26a-26c are installed about each container 61a-61c. A pipe 29 is connected to each of the containers 61a to 61c. The position to which the pipe 29 is connected is the first fluid upstream side of the first heat exchange units 22 a and 22 b and the second heat exchange unit 23.

  Although the case where two first heat exchange units are provided is illustrated in FIG. 5, one or three or more first heat exchange units may be installed.

In the saturator 60 of the second embodiment, heat exchange is performed in the same manner as the case 1 of the first embodiment.
That is, in the second heat exchange part 23 of the container 61c, heat exchange is performed between the first fluid (temperature T ₉ ) flowing in the flow passage and the third fluid. The heat exchanger, the third fluid is cooled to a temperature T _2.

Third fluid that has been cooled to a temperature T ₂ flows through the conveying path 25, and flows as the first fluid into the container 61a from the container 61a upper to.

The spraying part of the humidifying part 26a sprays water on the first fluid before flowing into the first heat exchanging part 22a. The sprayed water comes into contact with the first fluid (temperature T ₂ ) and evaporates, water vapor is added to the first fluid, and the first fluid reaches temperature T ₃ .

The synthesis gas as the second fluid discharged from the reaction tube 3 is cooled to a temperature T ₁₁ (about 300 to 400 ° C.) and then supplied to the first heat exchange unit 22b of the container 61b.

In the first heat exchange units 22a and 22b, heat exchange is performed between the first fluid and the second fluid. The first fluid is heated from an inlet temperature _{T 3} on the outlet temperature _{T 4} at the first heat exchanging portion 22a, it is conveyed from the container 61a to the vessel 61b through the pipe 62a. The first fluid is heated from an inlet temperature _{T 5} at the first heat exchanging portion 22b in the outlet temperature _{T 6.}

The second fluid is cooled from the temperature _{T 11} to _{T 13} in the first heat exchange portion 22b, it is conveyed from the container 61b to the container 61a via the pipe 24. The second fluid is cooled from the temperature _{T 13} to the temperature _{T 14} in the first heat exchange portion 22a. The second fluid is discharged from the saturator 60 as the temperature _{T 14.}

  Also in the second embodiment, the water sprayed from the spraying sections of the humidifying sections 26a and 26b becomes water vapor by the heat of the first fluid and the second fluid in the first heat exchange sections 22a and 22b. Thereby, the first fluid is heated while maintaining the saturated vapor pressure when passing through the first heat exchange units 22a and 22b.

First fluid has reached the temperature _{T 6} passes through the first heat exchanging portion 22b, through the vessel 61b pipe 62b flows into the container 61c as the temperature _{T 9.} In the second heat exchange portion 23 of the container 61c, the first fluid is heated to a temperature _{T 10} from the temperature _{T 9} Replace third fluid and heat. At this time, since water is sprayed from the upper side of the second heat exchange unit 23 by the spray unit of the humidifying unit 26c, the first fluid passing through the second heat exchange unit 23 is heated while maintaining the saturated vapor pressure. The

First fluid which has passed through the second heat exchanger 23, with steam of saturated vapor pressure, and is discharged from the saturator 60 as the temperature T _10.

As described above, the saturator 60 shown in FIG. 5 is subjected to the same heat exchange as that of the case 1. Therefore, the temperatures T _{1 to} T ₁₄ in the saturator 60 are substantially the same as those of the case 1 in Table 1. That is, it is possible also in the second embodiment, to increase the first fluid temperature T ₁₀ of after being heated by the saturator. Further, it is possible to reduce the temperature T ₃ of the first fluid in the first heat exchange portion 22a upstream.

DESCRIPTION OF SYMBOLS 1 Natural gas reforming system 2 Reformer 3 Reaction tube 4 Reforming furnace 5 Waste heat recovery part 6 Chimney 7, 8, 24, 29, 62a, 62b Pipe 9 Waste heat boiler 10 Natural gas supply line 20, 30, 60 Saturator 21 Tower 22a, 22b 1st heat exchange part 23 2nd heat exchange part 25 Conveyance path 26a, 26b, 26c, 26d Humidification part 27a, 27b, 27c Storage part 28a, 28b, 28c Pump 61a, 61b, 61c Container

Claims (4)

A flow path through which the first fluid circulates;
One or more installed along the flow direction of the first fluid in the flow passage, and a first heat exchanging unit that exchanges heat between the first fluid and the second fluid;
Between the first fluid and the third fluid, which is installed on the downstream side of the first heat exchange part in the flow direction of the first fluid in the flow passage and passes through the first heat exchange part. A second heat exchange part for heat exchange;
A humidifying unit for adding water to the first fluid flowing in the flow path on the upstream side of the first fluid of the first heat exchange unit and the second heat exchange unit;
The third fluid after heat exchange in the second heat exchange section is transported from the second heat exchange section to the first fluid upstream side of the first heat exchange section, and the circulation as the first fluid A conveyance path to flow into the path,
In the first heat exchange unit, the first fluid is heated and humidified, the second fluid is cooled and discharged out of the system,
A saturator in which, in the second heat exchanging section, the first fluid is heated, humidified to a saturated vapor pressure, discharged outside the system, and the third fluid is cooled.   2. The saturator according to claim 1, wherein the flow path is one tower that houses the first heat exchange unit and the second heat exchange unit.   2. The saturator according to claim 1, wherein the flow path is a pipe that connects a plurality of containers and the containers, and each of the first heat exchange unit and the second heat exchange unit is accommodated in the container. . A reformer that reacts the natural gas, which is the first fluid, with water vapor to produce synthesis gas containing hydrogen, carbon monoxide, and carbon dioxide, which is the second fluid;
A natural gas supply line for supplying natural gas as the third fluid;
A natural gas reforming system comprising the saturator according to any one of claims 1 to 3.

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